High pressure alkylation reaction



Patented Aug. 10, 1943 HIGH PRESSURE ALKYLATION REACTION Hans o. Vesterdal, Elizabeth, N. 1;, assignor to Standard Oil Development Oompany, a corporation Delaware No Drawing. Application October 5, 1940,

Serial No. 359.895

Claims. (01. 280-;883-4) The present invention relates to the alkylatlon and/or polymerization reactions in which isoparainns are condensed with oleflns and/or olefins ar condensed with either similar or dissimilarolefin molecules to; yield normally liquid, branched chain, saturated and/or unsaturated hydrocarbons which flnd uses as blending agents and have direct application to utilization in the production or motor ruels.

It is known to condense isoparamns with olefins and to condense olefins with similar or dissimilar olefln molecules to produce alkylation reaction products and/or polymerization products. 'Ihisfhas been done thermally, that is,-by the application of heat alone, and it has also been accomplished by resorting to the use of certaincatalysts under quite varying reaction conditions. Among the catalysts employed for eilecting conliquid hydrocarbon condensation products, the said reactions being catalyzed by the presence oi one or more substances taken from the group consisting oi oxides and sulfides or metal; or zrouns 5.6 and'lortheperiodicsystem. mearrying out this process it is necessary, however, in order to carried out in the presence of a mixture oi these two substances. Fundamentally. the reaction is den'sation oi oleiins, either-with themselves or with iso, may be mentioned concentrated sulfuric'acid, aluminum chloride with or without the use 0! hydrogen halide; and various other Friedel-Crafls typ catalysts. boron fluoridewater mixtures and their resulting chemical compounds-phosphoric acid either alone or deposited on carriers such as kieselguhr and the like, and various-other similar compounds.

The process oi the present invention is prl marlly. concerned with the production 01" normally liquid, branched chain, substantially completeiy saturated hydrocarbons boiling within the motor iuel boiling range," but is of necessity concerned Wit- 11118 production of polymers or olefins sinceLthe reaction taking place according to the process-roisthe' present invention is not one of alkylation tothe exclusion or one of polymerization. In other words, while it is possible to produce substantial quantities of polymers in the ,reaction mixture. nevertheless it is an object or the present invention to so manipulate the reaction conditions, catalyst, reactants, etc., to obtain as high yields as possible or the desired alkylates. The product as prepared according to the present invention therefore predominates in satu- .rated. branched chain, normally liquid hydrocar- The process 0! the present invention may be in general described as eflectlng a condensation between at least one iso and at least one olefln, preferably a monoolefln, and/or a condensation between an olefin, preierablya monoolefln, and another olefin either of similaror dissimflar configuration, these two types or reaction beins carried out simultaneously under reaction conditions conducive to the production or normally bium and tantalum. It 1 a vapor phase process. However, under certain restricted specific reaction conditions where a proper choic of reactants has'been made it may be possible and at times desirable to carry out the reaction in the liquid phase. Ordinarily, however, vapor phase reaction is preferred.

The various catalysts which are contemplated may-be iurther defined as including the oxides and sulfides oi' manganese, chromium, molyb denum, tungsten, uranium and vanadium, column;

4 :e: i and last at times undesirable, to employ any one'oi these specific compounds as the catalyst. It'is oftentimes desirable to employ a mixture of two or more 01' these catalysts. "For example, chromium and molybdenum oxides may be employed, vanadium and chromium oxides, vanadium and molybdenum oxides, or ath ree-component catalyst such as. for example. vanadium, chromium and molybdenum oxides. ,It is within the s op of the present invention to employ yst of oxides and sulfides, for example. chromium oxide admixed with molybdenum sulfide. However, in promoting this reaction with either water,

hydrogen sulfide, or mixtures of water and hydrosen sulfide, it is well to keep inmind that under theusual reaction conditions it suiilcient amounts of hydrogen sulfide are present as promoter eventually .the oxide ca y into the co sulfide In the preferred ,embodimentof invention the oxide catalysts arepreterred, oi their increased activity with to tion but also because 01 ct other advantage to the use particularly whenusedin tar as the promoter, and the recovery or the desiredflnsl' cases wheresulndesandsulll'lecre talyst be converted,

in the reaction. it is oftentimes necessary to resort to an alkali wash in order to remove from the final product dissolved sulfur compounds, whereas in connection with the use of oxide catalyst with a water promoter it is unnecessary to subject the final desired product to such purification treatment.

Although the above described catalysts may be employed alone in the process of the invention, it is desirable particularly in commercial operations and from the economical standpoint to employ the catalyst in conjunction with a carrier. The types of carrier employed may be quite varied in nature and although no determination has been made it is felt that in some instances the carriers are not inert in the reaction and in some manner contribute to the ultimate final yield of the desired products. Carriers may be either of the porous or non-porous type. although since the reaction embodyingthe invention is thought to be essentially a surface reaction it is preferred to employ the porous carriers. These carriers are of the type such as clays, either natural or acid activated, the gels such as, for example, alumina gel or silica gel, bauxite, fullers earth, bentonlte, kieselguhr, pumice, celiie, montmorillonite, rsil, tonsil, Super Fiitrol, activated ficridin, activated charcoal or activated carbon; and various other types of carriers such as pieces of porcelain or chemical stoneware and the like may be employed.

Various methods may be employed in depositing the heretofore mentioned oxides and sulfides on the carriers. In general, the oxides are deposited upon the porous carriers by the impregnation of said carriers, for example, silica gel or alumina gel, by admixing with the corresponding hydro gels salts of the various metals which upon thermal treatment decompose to give the desired oxides. The sulfides of the above-mentioned metals maybe incorporated in the porous carriers by precipitating the aforementioned metal salts on the hydro gels and heating in the same manner as the oxides are produced. This catalyst mass may be then treated with hydrogen sulfide, ammonium sulfide, or some equivalent sulfide compound in order to convert the metal oxides to their corresponding sulfides. Mixtures of two or more of the porous carriers may be employed as, for example, a mixed alumina-silica. gel or an activated carbon admixed with an alumina or silica gel. In connection with the deposition of the meta; oxides or sulfides on the non-porous type carriers, it is sometimes advantageous to employ a binder. Generally. however, a wetting of the non-porous carrier followed by drying or thermal treating to convert to the oxide is suincient to leave a coating on the carrie; which is adequate ,i'or use in the reaction. The amount of oxides and/or sulfides oi the metals of the filth, sixth or seventh groups of. the periodic system deposited may vary considerably with reheet to the carriers mployed. In general, however, the ultimate percentage of oxide and/or sulflde oflthe impregnated in or deposited on these carriers varies between about 1% and about or .e'v as high as preferably between 7% 1% by weight of the amount of carrier have been made em- Ployin'gh, wherein the metal oxides or u id s as hi h as. oi, t t l w lsht bf catalys m tim m o r nt ses o1 mtalor dem e an. he V3.11? s; carriers depends to some extent ut n i s. available beef-area or the carrier employed..

assumes Also, depending upon the reaction conditions, the amount of catalytic component of the catalyst mass may vary considerably. v Thus, when carrying out the reaction under-drastic reaction conditions a lesser amount of the catalytic component of the catalyst mass is ordinarily required than is the case where the reaction is carried out under milder reaction conditions, in which case a larger portion of the catalyst mass is preferably the active catalytic component.

The catalyst may be prepared in any desired form such as, for example, pills, pellets, briquettes or powder, or some other finely divided or comminuted form. It is likewise possible and at times preferred to extrude the catalyst composition, particularly where the gels are employed, in the form of the hydro gels through orifices of predetermined size. The extruded catalyst is then heated to drive oil the water and to decompose the metal salts to the corresponding metaloxides or sulfides.

The specific oxides and sulfides employed in the process of the invention may vary in form depending upon the degree of oxidation of the particular metal. In general it is proposed to employ those oxides and sulfides of metals which constitute at least theoretically the acid anhydrldes of those metals employed. Thus, for example, CrzOa is employed since it is considered to be the acid anhydride of chromous acid. CrOa is employed since it is considered to be the acid anhydride of chromic acid. Similarly, M00: is

employed as being the counterpart of molybdlc acid. This analogy likewise applies to the sulfides since, for example, M05: is considered the acid anhydride of thiomolybdic acid and Grass is considered the acid anhydride oi thiochromous acid. Various other oxides and sulfides of chromium may be employed. Thus, for example, CIOOr, CrS and CraS4 may be employed. In the case of vanadium oxides and sulfides, the compounds customarlly employed are V285, V283, V282, V205, V204, V203 findVaOz. The manganese compounds include MnSe, MnS, MnzOa, M1201, M1102, etc. It should be distinctly understood, however, that although no definite information is to be had at the present time, these various oxides and sulfides when deposited on the carriers and employed in the reaction under the hereinafter specified reaction conditions are very probably altered in their chemical structure by reason of the reaction conditions to the more stable oxides and sulfides.

A catalyst of the type employed may be prepared by co-precipitating the hydroxide of aluminum and chromium wherein the molar ratio of aluminum to chromium is ultimately to be about 2:1 with ammonia'from a solution oi the aluminum and chromiummtrates. The resultant gel is washed and dried.:molded orpressed into the desired shape, {or example, pills, and then heated to alnn i;i300 Rio: a length of time sumcient to substantially rompletelysdehydrate the same. To prepares. moiyhdenum oiddevcatstthe h d xide o sulllmlnumwwas fink ere'nated with an aqueous solution -cr ams monium molybdate sufiicient so that the catalyst will contain about 9%. fiiimq libflihsolddmin nal pro uc T mass naewssned and he te or, atoutso at dzflflial 'smea y a mbnmietted ath des red pe let ,forpi :Iueilhsmimthe: Most v lam tain d was th n 1' i i-1 t e catal st which foiiirdnus'eix inthepresent reaction'wass hydroxide and adding thereto a. suificient amount oi an aqueous solution oi ammonium vanadate and homogenizing the same. The resultant mass was then washed, freed of excess water, pilled and then heated to about 800 F. for about 3 hours. This composition contained about 1.7% of vanadium pentoxide. The weight ratio of silica to alumina was maintained at about 1.7:1.

The reaction may be carried out using a variety oi reactants. It is necessary that at least one of the reactants be an isoparaflin, that is. a paraiiinic hydrocarbon containing at least one tertiary carbon atom per molecule. Such compounds as isobutane, isopentane and higher homologues are suitable as one oi the reactants in the process. Mixtures of two or more oi the isoparafiins may likewise be employed. particularly wheresaiety fuels and aviation naphthas and the like are the desired final products. The presence of normal parailins in admixture with isoparaifins is in no wise detrimental to the activity of the isoparaiilns. In fact, there is some indication that a portion at least of the paraffinic constituents oi the feed stock may to some extent become dehydrogenated duringthe reaction to form the corresponding olefinic compounds. Not only are the corresponding oleflnic compounds though to be formed but likewise to some extent at least it is thought that the parafflns either of the branched or straight chain type undergoing dehydrogenation may be isomerized to the corresponding straight or branched chain type, as the case might be. Although a such the normal paraifins appear to be substantially inert in the reaction as herein indicated, they may to the-extent to which they are isomerized and/or dehydrogenated prove a distinct benefit by their presence in the reaction feed stock.

The olefinic reactants may be selected from a number of the common oleiins present in refinery ases and to be found elsewhere as well. 'For example, ethylene, propylene, normal butylenes, isobutylene, the isomeric pentenes, and similar higher monoolefinic hydrocarbons oi either a straight chain or branched chain character, may be employed. Mixtures of two or more of these olefin may be employed as the oleflnic components of the feed stock. It is generally preferred to employ normally gaseous oleflns as the reactants but this is chiefly because of economic factors. Normally liquid monoolefins, however, are equally desirable. Such oleflns are polymers, copolymers, interpolymers, etc., oi the above-mentioned monoolefins, these being, for example, di-

isobutylene, triisobutylene, the polymers resulting from the condensation of normal butylenes with isobutylene, of butadiene with butylenes, and the like. L

Suitable sources oi the various olefins and isoparaflins are to be found in the gases coming from the thermal and/or catalytic cracking .units oi an oil' refinery, from field butanes which have been subjected to prior isomerization and/or partial dehydrogenation treatments, irom refinery stabilizer bottoms, from stabilizer overhead gases, etc. In general, it is preferred to employ a molar excessoi the isoparamnic component oi the feed stock with respect to the total oleflnic content 01' that ieed stock. A molar. ratio or isoparailins to oleflns or at-least 2:1 and preierably of at least 5:1 is desirable. Molar ratios running as high as :1 are, however, within the scope of the present invention, although it is to be understood that equal molar ratios may be employed without attendant sacrifice in quality oi the product in some instances.

The process may be carried out either as a batch, continuous or semi-continuous type oi operation. Economic considerations make it preferable to carry the process out in a continuous manner, especially where the process is operated on 'a commercial scale. The reaction mixture should be intimately contacted with the catalyst since the reaction is apparently a contact type and higher yields 01 the desired product are obby a vigorous and intimate mixing or tion oi the reactants in the presence of and ontact with the catalyst mass under the reaction conditions. In general, however, under the reaction conditions this degree of agitation is attained without the use of any external or mechanical means of agitation being employed. No particular type oi apparatus is required to successfully carry out the reaction. Equipment customarily employed for the catalytic. dehydrogenation of paraflinic hydrocarbons under superatmospheric pressures or for the high presure hydrogenation processes which are well known may be employed to advantage in carrying out the present process.

The temperature under which the reaction is maintained may vary considerably. The rea-c tion is carried out under temperatures ranging between about 375 F. and about 950 F., preferably between about 575 F. and about 800 F. It is realized of course that with each particular type of catalyst employed the optimum temperature varies considerably but in general the above temperature ranges are adequate for carrying out the reaction to give the desired motor fuel products.

The process is carried out under fairly high superatmospheric pressures. Pressures ranging between about 500 and about 16,000 pounds per square inch, preferably between about 1500 and about 14,000 pounds per square inch, are firm ployed. The time of contact of the reactants with the catalyst under the temperature and pressure conditions above mentioned may vary considerably depending upon the temperature. pressure and nature of the reactants employed. In general, the time of contact lies between about 1 and about 60 minutes, preferably between about 10 and about 30 minutes. Reasonable care should be exercised in correlating the abovedeflned reaction conditions together with the type of feed stock employed so as to avoid substantial cracking or carbonization of the hydrocarbons ied to the reaction zone. Obviously, a temperature as high as 950 F. with a pressure of around 500 pounds per square inch and a time of contact of around 60 minutes would quite extensively carbonize and crack a feed stock containing Co and C1 isoparafllns in conjunction with Cu or 012 monooleiins. Likewise, the conditions should be suiiiciently drastic to cheat a substantial condensation of the oieflnic components of the feed stock principally with the isoparafiinic components of that feed stock or at least with another portion of the same or difl'erent oleflnic components of that feed stock. In other words, an extremely mild condition when employing diisobutylene with Co and C1 isoparailins, that is, a contact time of around 1 minute when using a. pressure of around 500 pounds per square inch V and a temperature of around 375 F. would obviously not be suflicient to produce the desired result. Suiiice it tosay that the optimum reaction conditions iqr any particular feedstock to give the desired final products are best determined for any particular catalyst employed by one or two trial runs at varied temperatures, pressures and times of contact within the ranges heretofore outlined and in accordance with the principles of the invention as heretofore stated.

The amount of hydrogen sulfide and/or water added to the reactants or conducted directly into the reaction zone varies to a certain extent depending upon the amount of active catalyst present in the catalyst composition. In general, the amount of promoter added to the reaction or present in the reaction zone at any one time should be between about 0.5% and about 20% by weight of the catalyst mass, preferably between about 5% and about by weight. As

will be understood from the hereinafter described runs under the particular reaction conditions therein outlined, about 10% by weight of water was found to be optimum therein. As a general guide in determining the amount of hydrogen sulfide or water to be present in the reactor at any one time, it may be stated that sufficient promoter should be present in contact with the catalyst to at least afford a monomolecular him of the promoter in contact with the active surface of the catalyst mass.

After prolonged usage of the catalyst mass in the present reaction, in some cases after usages mounting to as long as 4,000 hours, the catalytic activity becomes somewhat impaired.- The addition of elemental oxygen or elemental sulfur, depending upon whether the catalyst employed is an oxide or a sulfide, will to some extent, reactivate the catalyst. The inactivity of the catalyst after prolonged usage has been thought to be due largely to an accumulation or building up and clogging of the pores of the catalyst or covering of the catalyst surface with carbonaceous deposits. The introduction of oxygen or sulfur, particularly where the carbonaceous deposits are of a soft or gummy consistency, will in some cases purge the mass of these deposits, and although not completely reactivating the mass, will substantially revivify the same and fit it for further usage in the reaction. In order to completely reactivate the catalyst once its catalytic activity has become substantially impaired, the catalyst is withdrawn from the reaction and, in the case of the oxide catalysts. the original activity may be restored by the introduction of air or oxygen either diluted withinert gases such as, for example. nitrogen'or carbon dioxide or steam, at temperatures of between about 800 F. and about 1800' F. for a sufilcient length of time to enable the rapid oxidation of the carbonaceous material to substantially completely remove the same from the pores and from the surface of the catalyst mass. This introduction of free oxygencontaining materials should be controlled so that the regeneration follows a fairly even course and avoids the burning of! of the n'arbo us than at erratic rates since the heat of combustion is difllcult to remove where the oxidation process becomes too rapid. After the carbonaceous material has been the catalyst is then ready for reuse in the reaction. This method of regeneration is simpiyliilustrative of any number of conventional sccept methods for regenerating catalysts employed in hydrocarbon reactions and the process of the invention is by no means iimitedor restricted to the described regenerative method. -Any suitable regenerative method maybcemplo a The regeneration or reactivation of the sulfide it of 'the reaction. the

a,aac,ses

catalysts may require a somewhat different type of treatment. The above-described process for regeneration of the oxide catalysts may he resorted to and the resultant reactivated catalyst mass which finds the metal in combination with oxygen rather than sulfur is then dissolved in ammonium hydro sulfide and treated with hydrogen sulfide to form the ammonium thio metallate. Acidification of this mass with sulfuric acid precipitates the metal sulfide which is then heated inthe presence of a reducing gas such as, for example, free hydrogen, at between about 500 F. and about 800 F. to form the more stable and more active metal sulfide catalyst. This material may then be formed into pills and the like or it may be directly reused in the process of the invention.

As illustrative of the method of carrying out the process of the invention, but without unduly restricting the invention to the scope specifically disclosed, the following examples are submitted:

Example 1 .there was charged about432 grams of isobutane and over a period of about 16 minutes there was gradually added about 102 grams of propylene. The bomb was shaken and the heating was continued for an additional 30 minutes. The final temperature of the bomb was about 735 F. and the final pressure was about 11,000 pounds per square inch, the pressure at the end of the propylene addition having been about 14,000

pounds per square inch. The reacted mixture was removed from the bomb and the normally liquid product constituting the 05+ fraction was isolated and constituted a yield of about 160% based on the total propylene reacted and a yield of about 05% based on the total propylene charged to the reactor. This product amounted to about 107.5 grams and the producacorresponding to the Cr-Cs fraction amounted to about 54% of the total normally liquid product and had a bromine number of about 39. The residue amounting to about 48% of the product recovered had a bromine number of about 30. An

increase in the Cs-Cil component of the product could be obtained in this run if the olefin had been added more slowly and a higher molar ratio of isobutane to propylene had been maintained in the reaction zone. The isobutane to propylene molar ratio actually amounted to about 3: 1 as the run was carried out.

Under comparable conditions, except that no water was added to the catalyst mass prior 'to aid of normally liquid product amounted to a 50% based upon the olefin charged, or about based upon the olefin wnsumed. The (it-Ga fraction in this particular run was about 44% of the normally liquid product recovered and it had a bromine number of about 69.

Under comparable conditions, except that. no catalyst was employed and no water was added. thekh zrodnct obtained amounted to about 43% olefin charged or about 06% of the plefin or 17, innoontrast to a accuses some out 01 about 89 when employing water and the catalyst, it would appear that to some extent at least a dehydrogenation reaction had occurred when the catalyst and water were employed in the reaction. 7 likewise, where the water was absent buta catalyst was employed, the bromine number or'the C-C8 cut was higher than when the water was employed. In that case the bromine number was 69, whereas in the "case where water was employed the bromine numberwasabout39. g

The use of 5% water under comparable conditions gave substantially the same yield or normalhrliquid product as when water was absent. However, "the; (ls-Cc out in the normally liquid product was 53.8%.and the bromine number was about 61. when using about 20% of water, the other reaction conditions being comparable to those specified in Example 1, the yield of normally liquid product constituted about 48% or the propylene charged to the bomb or about 141% based upon the propylene consumed and the Cs-"Cs traction amounted to about 55.5% 'oithe normally liquid product and this fraction had a brominenumber of about 49.

V U Q f "f f. j'rample 2 J A bomb oi the same type as specified in Examplei waacharged with the same catalyst employed in "Example- 1 in substantially the same amount. To thiscatalyst there was added about 11% .by weight of water. The catalyst composition together with the promoter was then heated to a temperature of about 770 F. and

about 386 gramme! isobutane were charged to the reactor under a pressure of about 7,000 pounds peresqnarcinch. About 101 grams of propylene were slowly added over a period or 16 ,minuws toitheecatalyst and isobutane mixture and the pressure rose from about 7,000 pounds per square inch to about 12,400 pounds per square inch and the temperature remained substantially the same. The bomb was shaken and the heating was conthiued for an additional 30 minutes, at the end 01' which time the pressure had dropped to about 9,000 pounds per square inch withthe temperature being maintained at 510111111 770' F. The normally liquid product amounted to about 87.4 grams and this amounted to a yield of about 07% based on the propylene charged or about 135% based on the propylene consumed. The Cs-Ca traction amounted to about 57.5% or this product and it had a bromine number of about 84. The residue likewise had a'bromine number 01' about 34.

trample 3 Abombsimilartothatemployedinitxamples 1 and 2 was charged with about the same amount of a catalyst prepared by co-precipitatlng aluminum hydroxide and chromium hydroxide with ammonia rroma solution of aluminum and chromium nitrates. The co-precipitated gel was washed, dried. pilied and heated'to about 800 F, and the relative amolmts oi the chromium and aluminum compounds employed were such as to yield a resultant chromium oxide:aluminum oxide ratio or about 1:2. To this catalyst there was added about 11% by wei ht orwater. The

bromine number for the was maintained at a catalyst was introduced into the bomb which temperature of about 760 F. and to this catalyst mass there was added about 393 grams of isobutane. while maintainin: the pressure at about 7,400 pounds per square inch there was added about 116 grams 01' L propylene gradually over a period or about 18 weight Of V's-O4.

about 115.4% of minutes, during which time the pressure rose to about 12,800 pounds per square inch. The bomb was shaken and the heating continued for an additional 30 minutes. The final temperature oi the bomb was about 770 F. and the final pressure was about 9,000 pounds per square inch. The normally liquid product recovered from the reaction mixture amounted to about 118 grams which constituted a yield of about 101.5% based on the propylene charged or a yield of about 144% based on the propylene consumed. The Cs-Ca cut obtained from this product amounted to about 57.3% and had a bromine number of about 25. The residue had a bromine number of about 29.

Under comparable conditions. except that the temperature was maintained at around 700 F. but no water as a promoter was employed in conjunction with the catalyst, the normally liquid product obtained amounted to about 36% based upon the propylene charged or about 92% based on the propylene consumed. The C's-Ca fraction which amounted to about 41.2% of the recovered product had a bromine number of about 51.

Example 4 To a bomb maintained at a temperature oi about 700 F. there was added the same amount oi catalyst as was employed in the preceding examples. This catalyst was prepared by homogenizing a silica hydro gel with aluminum oxide and adding thereto suflicient ammonium vanadate so that upon subsequent treatment the catalyst mass would contain about 1.69% by The homogenized mixture was dried, pilled and then heated to about 800 F. for about 3 hours. The weight ratio of silica to alumina was about 1.7 to 1. To this catalyst there was added about 11% by weight or water and admixed with this catalyst mass was 365 grams of isobutane. To this reaction mixture there was slowly added over a period or about 19 minutes, while maintaining the reaction mass at a temperature of between about 700 F. and about 720 F., about 115.8 grams of propylene. The vpressure rose from an initial pressure of about 7,000 pounds per square inch to around 14,000 pounds per square inch. The bomb was shaken and the reaction mixture was maintained under these reaction conditions for an additional 30 minutes, at the end of which time the temperature was around 720 F. and the pressure was about 13,000 pounds per square inch. A normally liquid product was recovered in an amount or about 100.7 grams which amounted to about 87.2% o! the propylene charged or tbbpropylene reacted. or this product about 55.8% constituted the Cs-Ca fraction. It had a bromine number oi 54, while the residue had a bromine number 01 about 10.

The nature and objects oi the invention havlns been thus fully described and illustrated.

what is claimed as new and useful and desired 6 assesses carrying out said reaction at temperatures between about 375 F. and about 950 F. under superatmospherio pressures in contact with a catalyst whose essential components are selected from the group consisting of oxides and sulfides of metals of group of the periodic system, and in the presence 01' a small amount of at least one compound having the formula nix. wherein x is a member or the group consisting oi oxygen and sulfur.

2. A process as in claim 1 wherein the time of contact 01' the reactants with the catalyst under the reaction conditions is conelated to avoid substantial carbonization and cracking.

3. A process which comprises reacting an isowith a monoolefln at a temperature between about 375' 1''. and about 950 F. under superatmospheric pressures between about 500 and about 16,000 pounds per square inch for between about & and about 60 minutes while correlating the reaction conditions to avoid substantial cracking and carbonization, in contact with a catalyst mass whose essential components are taken from the group consisting of oxides and sulfides of a metal oi'group 0 o! the periodic system. and in the presence 01 between about 15% and about 20% o! the catalyst weight 01' a oompound nix, wherein x is a member of the group consisting of oxygen and sulfur.

4.Aprocessasinc1aim3whereintheisoparamn is present in molar excess over the olefin and the catalyst is molybdenum oxide on alumina.

5. A process as in claim 3 wherein the isois present in molar excess over the olefin and the catalyst is a chromium oxide onalumina.

8.Aprocess as inciaim 8 wherein them' compound is added to the feed and the process is carried out continuously.

7. A procss which comprises condensing isobutane with at least one normally gaseous oleiln at a temperature between about 550 F. and about 000' I. under a superatmospheric pressure between about 1000 and about 14.000 pounds per square inch for between about 10 and about 30 minutes in contact with a catalyst mass whose essential components are selected from the group of the catalyst mass o! a member oi the group consisting of hydrogen sulfide and water, correlating the reaction conditions to avoid substantial cracking and carbonization and recovering normally liquid product.

8. A process which comprises condensing a reiinery 04 cut containing isobutane, iso and normal butylenes and normal butane in which the isobutane is present in a substantial molar excess over the total 01 oleiins present therein, at a temperature between about 050 F. and about 900" F. and under a pressure of between about 1000 and about 14,000 pounds per square inch for a period between about 10 and about 30 minutes in contact with a catalyst mass whose essential component is an oxide of a metal oi group 6 oi the periodic system, which contains added thereto about 11% by weight oi water, and recovering substantially saturated. branched chain,

normally liquid hydrocarbons irom the reacted mixture.

9. An improved process for alkylating oleilnic hydrocarbons with an isoparamn, comprising subiecting the olefin and isoparamn to the action of a catalyst, comprising essentially only a 6th group metal oxide, under reaction temperature and superatmospheric pressure while in the presence 0! a small amount 01' a compound having the formula Hex, wherein X is a member 01' the group consisting of oxygen and sulfur.

10. An improved process for alkylating oleiinic hydrocarbons with an isoparamn, comprising subjecting the oleiln and isoparamn to the action of a catalyst, comprising essentially only a 0th group metal sulphide. under reaction temperature and superatmospheric pressure while in the presence 01 a small amount of a compound having the formula nix, wherein X is a member oi. the

\ group consisting of oxygen and sulfur. 

